System and method for cleaning hyrocarbon contaminated water

ABSTRACT

A system and method removes petroleum from water by cavitating the petroleum/water mixture with air bubbles; irradiating the cavitated petroleum/water mixture with an electron beam to create ozone within air bubbles; and filtering the water from the irradiated mixture.

PRIORITY INFORMATION

This application is a divisional application of co-pending U.S. patentapplication Ser. No. 15/062,769, filed on Mar. 7, 2016; said U.S. patentapplication Ser. No. 15/062,769, filed on Mar. 7, 2016, is a divisionalapplication of U.S. patent application Ser. No. 14/076,122, filed onNov. 8, 2013, (now U.S. Pat. No. 9,295,966); said U.S. patentapplication Ser. No. 14/076,122, filed on Nov. 8, 2013, is a divisionalapplication of U.S. patent application Ser. No. 13/552,831, filed onJul. 19, 2012 (now abandoned).

This application claims priority, under 35 U.S.C. § 120, from co-pendingU.S. patent application Ser. No. 15/062,769, filed on Mar. 7, 2016; saidco-pending U.S. patent application Ser. No. 15/062,769, filed on Mar. 7,2016, claiming priority, under 35 U.S.C. § 120, from said U.S. patentapplication Ser. No. 14/076,122, filed on Nov. 8, 2013; said U.S. patentapplication Ser. No. 14/076,122, filed on Nov. 8, 2013, claimingpriority, under 35 U.S.C. § 120, from U.S. patent application Ser. No.13/552,831, filed on Jul. 19, 2012; said co-pending U.S. patentapplication Ser. No. 13/552,831, filed on Jul. 19, 2012, claimingpriority, under 35 U.S.C. § 119(e), from U.S. Provisional PatentApplication, Ser. No. 61/509,152, filed on Jul. 19, 2011; U.S.Provisional Patent Application, Ser. No. 61/510,772, filed on Jul. 22,2011; and U.S. Provisional Patent Application, Ser. No. 61/673,064,filed on Jul. 18, 2012.

This application claims priority, under 35 U.S.C. § 120, from U.S.patent application Ser. No. 14/076,122, filed on Nov. 8, 2013.

This application claims priority, under 35 U.S.C. § 120, from U.S.patent application Ser. No. 13/552,831, filed on Jul. 19, 2012.

The entire content of co-pending U.S. patent application Ser. No.15/062,769, filed on Mar. 7, 2016, is hereby incorporated by reference.The entire content of co-pending U.S. patent application Ser. No.14/076,122, filed on Nov. 8, 2013, is hereby incorporated by reference.The entire content of co-pending U.S. patent application Ser. No.13/552,831, filed on Jul. 19, 2012, is hereby incorporated by reference.

This application claims priority from U.S. Provisional PatentApplication, Ser. No. 61/509,152, filed on Jul. 19, 2011. The entirecontent of U.S. Provisional Patent Application, Ser. No. 61/509,152,filed on Jul. 19, 2011, is hereby incorporated by reference.

This application claims priority from U.S. Provisional PatentApplication, Ser. No. 61/510,772, filed on Jul. 22, 2011. The entirecontent of U.S. Provisional Patent Application, Ser. No. 61/510,772,filed on Jul. 22, 2011, is hereby incorporated by reference.

This application claims priority from U.S. Provisional PatentApplication, Ser. No. 61/673,064, filed on Jul. 18, 2012. The entirecontent of U.S. Provisional Patent Application, Ser. No. 61/673,064,filed on Jul. 18, 2012, is hereby incorporated by reference.

BACKGROUND

Utilizing conventional refining methods and processes, only about 30-40%of a single barrel of crude petroleum can be effectively converted(cracked) into gasoline. With the higher demands for carbon-based energyproducts, such as gasoline, it is desirable to convert a greaterpercentage of the crude petroleum into gasoline.

To realize a higher yield of gasoline, the less valuable petroleumfractions of the refining process, such as naphtha and alkenes(unsaturated hydrocarbons) and bitumen, should be converted to gasoline.

More specifically, it would be desirable to provide a process thatenables the conversion of less valuable petroleum fractions of therefining process into high octane gasoline-like mixtures ofhighly-branched saturated hydrocarbons (alkanes).

Another issue is utilization of newly discovered deposits of natural gasfor production of transportation fuels. Indeed, natural gas converted tohigher molecular weight hydrocarbons provides a viable alternative tocrude oil not only as a source for transportation fuels but also as thesource of highly valuable and easily transportable specialty chemicalproducts.

A further issue with utilization of crude petroleum as a source ofenergy is the results of spills. Oil spills are a source of undesiredpollution to the surrounding environment which needs to be cleaned up,especially if the oil spill occurs in a body of water.

One conventional method for cleaning up oil spills in water is to addtoxic materials to break up the oil, causing the oil to submerge anddisperse. However, although the oil spill may appear gone, the oil hasmerely gone deeper, thereby making it more difficult to effectivelycollect and clean-up.

Therefore, it is desirable to provide a more efficient and less toxicmethod of water remediation in the oil drilling industry, in shaleprocessing, in tanker clean-up, and in water processing on land, both ofrecovered water from oil removal, semi-conductor water treatment,municipal water treatment, mining operations, and toxic remediation ofan environmentally damaged site.

BRIEF DESCRIPTION OF THE DRAWINGS

The drawings are only for purposes of illustrating various embodimentsand are not to be construed as limiting, wherein:

FIG. 1 illustrates a flowchart showing an example of a process forconverting natural gas to liquidized highly-branched hydrocarbons;

FIG. 2 illustrates a flowchart showing an example of a process forconverting linear long carbon chain fractions of crude oil to liquidizedhighly-branched hydrocarbons;

FIG. 3 illustrates a flowchart showing another example of a process forconverting linear long carbon chain fractions of crude oil to liquidizedhighly-branched hydrocarbons;

FIG. 4 illustrates a block diagram of a system for converting naturalgas or long carbon chain fractions of crude oil to liquidizedhighly-branched hydrocarbons;

FIG. 5 illustrates a block diagram of a cavitation system and anelectron beam/electron beam sustained non-thermal plasma dischargesystem;

FIG. 6 illustrates a block diagram of a cavitation system and a dualelectron beam/dual electron beam sustained non-thermal plasma dischargesystem;

FIG. 7 illustrates a block diagram of a cavitation system;

FIG. 8 illustrates a mobile cavitation/electron beam/electronbeam-sustained non-thermal plasma discharge system;

FIG. 9 illustrates an example of the effective power of a dual electronbeam/dual electron beam sustained non-thermal plasma discharge systemwith respect to a jet of small drops of water;

FIG. 10 illustrates a block diagram of an example of a solid wastetreatment system using a cavitation/electron beam/electron beamsustained plasma discharge system;

FIG. 11 illustrates a block diagram of another example of a solid wastetreatment system using a cavitation/electron beam/electron beamsustained non-thermal plasma discharge system;

FIG. 12 illustrates an example of a multiple electron beam/multipleelectron beam sustained non-thermal plasma discharge system;

FIG. 13 illustrates another example of a multiple electron beam/multipleelectron beam sustained plasma discharge system;

FIG. 14 illustrates an example of a portable shielding system for usewith an electron beam/electron beam sustained plasma discharge system;

FIG. 15 illustrates another example of a portable shielding system foruse with an multiple electron beam/electron beam sustained plasmadischarge system;

FIG. 16 illustrates a block diagram of an oil recovery system using anelectron beam/electron beam sustained plasma discharge system; and

FIG. 17 illustrates a donut shaped biomass processing system.

DETAILED DESCRIPTION

For a general understanding, reference is made to the drawings. In thedrawings, like references have been used throughout to designateidentical or equivalent elements. It is also noted that the drawings maynot have been drawn to scale and that certain regions may have beenpurposely drawn disproportionately so that the features and conceptscould be properly illustrated.

As illustrated in FIG. 1, natural gas is enriched with acetylene, atstep S10. It is noted that the natural gas may comprise methane gas.Moreover, the natural gas may comprise a gaseous mixture of methane,ethane, propane, butane, and pentane, or any combination thereof.

The enriched gaseous mixture (natural gas and acetylene) is irradiatedby electron beam or exposed to an electron beam sustained non-thermalplasma discharge, at step S20. It is noted that the electron beam may bea 1.0-2.5 MeV electron beam.

Below is a chemical representation of the introduction of an electronbeam or electron beam sustained non-thermal plasma discharge to agaseous mixture of low molecular weight hydrocarbons:

CH₄+C₂H₆+C₃H₈+C₄H₁₀+C₅H₁₂ +e ⁻

By exposing the gaseous mixture to the electron beam or an electron beamsustained non-thermal plasma discharge, the low molecular weighthydrocarbons, interact with electron beam generated molecular ions andradicals to create liquefiable higher molecular weight highly-branchedhydrocarbons. In this conversing process, light alkyne and alkeneadditives as well their molecular ions and radicals act as an effectivecarbon oligomerization and branching agents.

Below is a structural representation of an example of a liquefiablehigher molecular weight highly-branched hydrocarbon:

It is noted that hydrogen may be a byproduct of the irradiation andconversion process. Between steps S25 and S30, this hydrogen isseparated and removed from the irradiated gaseous mixture to furtherpromote formation of liquefiable higher molecular weight highly-branchedhydrocarbons.

It is further noted that if the liquefiable higher molecular weighthighly-branched hydrocarbons are mostly unsaturated hydrocarbons, as inthe case of pyrolysis oil vapors, the resulting mixture can be enrichedwith hydrogen and re-exposed to the electron beam/electron beamsustained non-thermal plasma discharge to further crack and saturate thehydrocarbons.

At step S30, the converted product is cooled so that the liquefiablehigher molecular weight highly-branched hydrocarbons are condensed forremoval, at step S40, as higher molecular weight highly-branchedhydrocarbons or highly-branched alkanes. The removed highly-branchedhydrocarbons have a high octane value which can be used as an additiveto or as gasoline. It is further noted that individual highly-branchedalkanes can be further separated from the said mixture via distillationprocess and used as highly-valuable specialty chemicals.

The remaining gaseous mixture can be re-introduced into the process atstep S10 and utilized as part of the base feedstock used to create thehigher molecular weight highly-branched hydrocarbons.

As illustrated in FIG. 2, long carbon chain fractions of crude oil(liquid) are cavitated with natural gas, at step S05. A more thoroughdiscussion of the cavitation process will be described below withrespect to FIG. 7.

It is noted that the natural gas may comprise methane gas. Moreover, thenatural gas may comprise a gaseous mixture of methane, ethane, propane,butane, and pentane, or any combination thereof.

It is further noted that the long carbon chain fractions of crude oilcan be cavitated with natural gas.

The cavitation process adds “gas bubbles” to the long carbon chainfractions of crude oil, which enable a more effective penetration of anelectron beam/electron beam sustained plasma discharge, as well asgeneration of highly reactive molecular ions and radicals inside saidgas bubbles.

The cavitated mixture is discharged through a set of nozzles to createjets of droplets of long carbon chain fractions of crude oil. Thedischarging of the long carbon chain fractions of crude oil through theset of nozzles further cavitates the mixture before the mixture isirradiated by an electron beam or exposed to an electron beam sustainednon-thermal plasma discharge, at step S15. It is noted that the electronbeam may be a 1-5 MeV electron beam.

By exposing the jets of droplets of cavitated mixture to the electronbeam or electron-beam combined with non-thermal plasma discharge, thelong carbon chain fractions are broken down (cracked) to shorter carbonchains.

Most of the produced shorter carbon chains will have less than ninecarbons and thus have a lower boiling points (T_(b)<126° C.), allowingthem to evaporate out of the mixture and captured for furtherprocessing. These shorter carbon chains (C₁ through C₈) become gaseousafter preheating and subsequent irradiation by the electronbeam/electron beam sustained non-thermal plasma discharge.

The shortened carbon chains that have more than eight carbons remain ina liquid state and are fed back to the cavitation process of step S05,while the gaseous shorter carbon chains are fed to a second cavitationprocess being further enriched with natural gas at step S17.

At step S17, the gaseous shorter carbon chains are enriched with naturalgas. It is noted that the natural gas may comprise methane gas.Moreover, the natural gas may comprise a gaseous mixture of methane,ethane, propane, butane, and pentane, or any combination thereof.Lastly, it is noted that the gaseous shorter carbon chains may beenriched with light alkynes (acetylene, etc.) and/or light alkenes(ethylene, etc.).

The enriched gaseous mixture is irradiated or exposed to an electronbeam/electron beam sustained non-thermal plasma discharge, at step S25.It is noted that the electron beam may be a 1.0-5.0 MeV electron beam.

By exposing the gaseous mixture to the electron beam/electron beamsustained non-thermal plasma discharge, the carbons based compoundsinteract to create liquefiable higher molecular weight highly-branchedhydrocarbons. In this reaction, admixture of light alkynes and alkenes,as well its molecular ions and radicals, can act as an effective carbonoligomerization and branching agents.

It is noted that hydrogen may be a byproduct of the irradiation andconversion process. Between steps S25 and S30, this hydrogen isseparated and removed from the irradiated gaseous mixture to furtherpromote formation of liquefiable higher molecular weight highly-branchedhydrocarbons.

It is further noted that if the liquefiable higher molecular weighthighly-branched hydrocarbons are mostly unsaturated hydrocarbons, as inthe case of pyrolysis oil vapors, the resulting mixture can be enrichedwith hydrogen and re-exposed to the electron beam/electron beamsustained non-thermal plasma discharge to further crack and saturate thehydrocarbons.

At step S35, the converted product is cooled so that the liquefiablehigher molecular weight highly-branched hydrocarbons are condensed forremoval, at step S40, as higher molecular weight highly-branchedhydrocarbons or highly-branched alkanes. The removed liquid mixture ofhighly-branched hydrocarbons, having a high octane value, can be used asan additive to or as gasoline. It is further noted that individualhighly-branched alkanes can be further separated from the said mixturevia distillation process and used as highly-valuable specialtychemicals.

The remaining gaseous mixture can be re-introduced into the process atstep S17 or step S05 and utilized as part of the base feedstock used tocreate the higher molecular weight highly-branched hydrocarbons.

As illustrated in FIG. 3, long carbon chain fractions of crude oil(liquid) are cavitated with natural gas, at step S05. It is noted thatthe natural gas may comprise methane gas. Moreover, the natural gas maycomprise a gaseous mixture of methane, ethane, propane, butane, andpentane, or any combination thereof.

It is further noted that the long carbon chain fractions of crude oilcan be cavitated with air.

The cavitation process adds “gas bubbles” to the long carbon chainfractions of crude oil, which enable a more effective penetration of anelectron beam sustained plasma discharge.

The cavitated mixture is discharged through a set of nozzles to createjets of long carbon chain fractions of crude oil. The discharging of thelong carbon chain fractions of crude oil through the set of nozzlesfurther cavitates the mixture before the mixture is irradiated orexposed to an electron beam, at step S15. It is noted that the electronbeam may be a 1-5 MeV electron beam.

By exposing the jets of cavitated mixture to the electron beam, the longcarbon chain fractions are broken down (converted) to shorter carbonchains.

Most of the produced shorter carbon chains will have less than ninecarbons and thus have lower boiling points, allowing them to evaporateout of the mixture and captured for further processing. These shortercarbon chains (C₁ through C₈) become gaseous after preheating andsubsequent irradiation by the electron beam/electron beam sustainednon-thermal plasma discharge.

The shorter carbon chains that have more than eight carbons (>C₈) remainin a liquid state and are fed back to the cavitation process of stepS05, while the gaseous shorter carbon chains are fed to a secondcavitation process at step S17.

At step S17, the gaseous shorter carbon chains are enriched with naturalgas. It is noted that the natural gas may comprise methane gas.Moreover, the natural gas may comprise a gaseous mixture of methane,ethane, propane, butane, and pentane, or any combination thereof.Lastly, it is noted that the gaseous shorter carbon chains may beenriched with acetylene.

The enriched gaseous mixture is irradiated or exposed to an electronbeam, at step S25. It is noted that the electron beam may be a 1-5 MeVelectron beam.

By exposing the gaseous mixture to the electron beam, the carbons basedcompounds interact to create liquefiable higher molecular weighthighly-branched hydrocarbons. In this reaction, acetylene can act as aneffective carbon branching agent.

It is further noted that if the liquefiable higher molecular weighthighly-branched hydrocarbons are mostly unsaturated hydrocarbons, theresulting mixture can be enriched with hydrogen and re-exposed to theelectron beam sustained non-thermal plasma discharge to saturate thehydrocarbons.

It is noted that hydrogen may be a byproduct of irradiation andconversion process. This hydrogen can be utilized in a subsequentirradiation event to saturate the liquefiable higher molecular weighthighly-branched hydrocarbons.

At step S30, the converted product is cooled so that the liquefiablehigher molecular weight highly-branched hydrocarbons are condensed forremoval, at step S40, as higher molecular weight highly-branchedhydrocarbons or highly-branched alkanes. The removed highly-branchedhydrocarbons have a high octane value which can be used as an additiveto or as gasoline.

The remaining gaseous mixture can be re-introduced into the process atstep S17 or step S05 and utilized as part of the base product used tocreate the higher molecular weight highly-branched hydrocarbons.

In FIG. 4, cavitation device 100 cavitates long carbon chain fractionsof crude oil (liquid), received through conduit 25, with natural gas,received through conduit 50. It is noted that the natural gas maycomprise methane gas. Moreover, the natural gas may comprise a gaseousmixture of methane, ethane, propane, butane, and pentane, or anycombination thereof.

It is further noted that the long carbon chain fractions of crude oilcan be cavitated with air.

The cavitation process adds “gas bubbles” to the long carbon chainfractions of crude oil, which enable a more effective penetration of anelectron beam/electron beam sustained plasma discharge.

The cavitated mixture is discharged through a set of nozzles to createjets of droplets of long carbon chain fractions of crude oil. Thedischarging of the long carbon chain fractions of crude oil through theset of nozzles further cavitates the mixture before the mixture isirradiated or exposed to an electron beam or electron beam sustainednon-thermal plasma discharge in radiation chamber 200. It is noted thatthe electron beam may be a 1-5 MeV electron beam.

By exposing the jets of cavitated mixture to the electron beam, the longcarbon chain fractions are broken down (cracked) to shorter carbonchains.

Most of the produced shorter carbon chains will have less than ninecarbons and thus have lower boiling points, allowing them to evaporateout of the mixture and captured for further processing. These shortercarbon chains (C₁ through C₈) become gaseous after preheating andsubsequent irradiation by the electron beam/electron beam sustainednon-thermal plasma discharge.

The shorter carbon chains that have more than eight carbons (>C₈) remainin a liquid state and can be optionally fed back to the cavitationdevice 100, while the gaseous shorter carbon chains are fed to a secondcavitation device 250.

In the second cavitation device 250, the gaseous shorter carbon chainsare enriched with natural gas. It is noted that the natural gas maycomprise methane gas. Moreover, the natural gas may comprise a gaseousmixture of methane, ethane, propane, butane, and pentane, or anycombination thereof. Lastly, it is noted that the gaseous shorter carbonchains may be enriched with light alkynes such as acetylene and alkenessuch as ethylene.

The enriched gaseous mixture is irradiated or exposed to an electronbeam or electron beam sustained non-thermal plasma discharge in a secondradiation chamber 300. It is noted that the electron beam may be a 1-5MeV electron beam.

By exposing the gaseous mixture to the electron beam, the carbons basedcompounds interact to create liquefiable higher molecular weighthighly-branched hydrocarbons. In this reaction, admixture of lightalkynes and alkenes, as well its molecular ions and radicals, can act asan effective carbon oligomerization and branching agents.

It is further noted that if the liquefiable higher molecular weighthighly-branched hydrocarbons are mostly unsaturated hydrocarbons, theresulting mixture can be enriched with hydrogen and re-exposed to theelectron beam sustained non-thermal plasma discharge to saturate thehydrocarbons.

It is noted that hydrogen may be a byproduct of irradiation andconversion process. This hydrogen can be utilized in a subsequentirradiation event to saturate the liquefiable higher molecular weighthighly-branched hydrocarbons.

In the cooling/extraction device 400, the converted product is cooled sothat the liquefiable higher molecular weight highly-branchedhydrocarbons are condensed for removal, through conduit 425, as highermolecular weight highly-branched hydrocarbons or highly-branchedalkanes. The removed highly-branched hydrocarbons have a high octanevalue which can be used as an additive to or as gasoline.

The remaining gaseous mixture can be re-introduced into the process atcavitation device 100 or second cavitation device 250, via conduit 450,and utilized as part of the base product used to create the highermolecular weight highly-branched hydrocarbons.

Cavitation device 10 of FIG. 5, cavitates long carbon chain fractions ofcrude oil (liquid), with natural gas. It is noted that the natural gasmay comprise methane gas. Moreover, the natural gas may comprise agaseous mixture of methane, ethane, propane, butane, and pentane, or anycombination thereof.

It is further noted that the long carbon chain fractions of crude oilcan be cavitated with air.

The cavitation process adds “gas bubbles” to the long carbon chainfractions of crude oil, which enable a more effective penetration of anelectron beam sustained plasma discharge.

The cavitated mixture is discharged through a set of nozzles to createjets of droplets (20) of long carbon chain fractions of crude oil. Thedischarging of the long carbon chain fractions of crude oil through theset of nozzles further cavitates the mixture before the mixture isirradiated by or exposed to electron beam or electron beam sustainednon-thermal plasma discharge 35 generated by high voltage generator 30.It is noted that the electron beam may be a 1-5 MeV electron beam.

By exposing the jets (20) of cavitated mixture to the electron beam 35,the long carbon chain fractions are broken down (cracked) to shortercarbon chains.

Cavitation device 10 of FIG. 6, cavitates long carbon chain fractions ofcrude oil (liquid), with natural gas. It is noted that the natural gasmay comprise methane gas. Moreover, the natural gas may comprise agaseous mixture of methane, ethane, propane, butane, and pentane, or anycombination thereof.

It is further noted that the long carbon chain fractions of crude oilcan be cavitated with air.

The cavitation process adds “gas bubbles” to the long carbon chainfractions of crude oil, which enable a more effective penetration of anelectron beam sustained plasma discharge.

The cavitated mixture is discharged through a set of nozzles to createjets of droplets (20) of long carbon chain fractions of crude oil. Thedischarging of the long carbon chain fractions of crude oil through theset of nozzles further cavitates the mixture before the mixture isirradiated or exposed to two electron beams or electron beam sustainednon-thermal plasma discharges (35 and 45) generated by two high voltagegenerators (30 and 40). It is noted that the electron beams may be a 1-5MeV electron beam.

By exposing the jets (20) of cavitated mixture to the electron beams (35and 45), the long carbon chain fractions are broken down (converted) toshorter carbon chains.

FIG. 7 shows a more detail example of a cavitation device 10. Thecavitation device 10 is divided into three stages or zones. In the firststage or zone 12, the cavitation device 10 cavitates long carbon chainfractions of crude oil (liquid), with natural gas, received by conduit11. It is noted that the natural gas may comprise methane gas. Moreover,the natural gas may comprise a gaseous mixture of methane, ethane,propane, butane, and pentane, or any combination thereof.

It is further noted that the long carbon chain fractions of crude oilcan be cavitated with air.

The first stage or zone 12 of the cavitation device 10 adds “gasbubbles” to the long carbon chain fractions of crude oil.

The cavitated mixture from the first stage or zone 12 of the cavitationdevice 10 is introduced into the second stage or zone 14 of thecavitation device 10. The second stage or zone 14 of the cavitationdevice 10 splits the “gas bubbles” from the first stage into smaller“gas bubbles.” The smaller the “gas bubbles,” the more effective thepenetration of an electron beam/electron beam sustained plasma dischargewill be.

The cavitated mixture from the second stage or zone 14 of the cavitationdevice 10 is discharged through a set of nozzles (16) to create jets(17) of long carbon chain fractions of crude oil. The discharging of thelong carbon chain fractions of crude oil through the set of nozzles (16)further cavitates the mixture before the mixture is irradiated orexposed to an electron beam or electron beam sustained non-thermalplasma discharge.

In the various embodiments discussed above, natural gas can be convertedto a mixture of highly-branched hydrocarbons, with average octane numberas high as 110, which is virtually non-existent in crude oil. Since themixture has a very high octane value, the liquid mixture can be utilizedas an additive to various gasoline formulations.

Moreover, in the various embodiments discussed above, the describedprocesses allow for the creation of a variety of outputs, includingliquid fuels as well as other additive ingredients such as solvents,etc.

Although the various embodiments discussed above focused on theintroduction of natural gas, other various feed stocks can be used. Forexample, adding a carrier gas, such as argon, may serve as an effectiveenergy transfer agent increasing efficiency of polymerization of lowmolecular weight hydrocarbons into higher molecular weight hydrocarbons,while also protecting just synthesized higher molecular weighthydrocarbons from an immediate destruction by the electron beam orelectron beam sustained plasma discharge.

It is noted that, in a full circulatory mode, a carrier gas remains incirculation as the carrier gas does not polymerize or condense inelectron beam driven gas to liquid conversion process.

In addition, ethylene gas may be added to serve not only as additionalenergy transfer agent but also as an effective branching agent. However,as a branching agent, ethylene will be extended in the process; andtherefore, the ethylene must be replenished together with natural gas.In this example, ethylene gas replaces acetylene gas mentioned as anoligomerization and branching additive in the previous embodiments.

Upon creating the mixture, the various individual components can beseparated by simple distillation using a conventional distillationcolumn process to separate each individual component from the entiremixture by heating the entire mixture up to the first distillation pointand keeping the temperature at this point for some time to allow fullevaporation of the first component with the lowest distillationtemperature. The vapor of the first most volatile component is thenremoved vapor and then the temperature is raised further to the nextdistillation point. The process is repeated until the very lastcomponent with the highest temperature remains in its liquid phase.

A high purification process may be implemented to raise the purity ofeach distillated component up to a pharmaceutical grade by usingmicrofiltration or even nano-filtration membranes as well as by otherpurification processes.

Another embodiment may include a serial circulation setup of electronbeam irradiation units, wherein each electron beam irradiation unit isfollowed by a hydrogen gas separator that lets the carrier gas withvapors to pass-through, followed by a liquid fuel product condenser andfinally by feed gas replenishment entrance before the next electron beamirradiation unit.

In the natural gas conversion to liquid fuels processes described above,the feed gases may include dry natural gas, wet natural gas, orassociated petroleum gas. The energy transfer enhancing gaseousadditives may include Argon, and the oligomerization and branchingprocess enhancing gaseous additives may include light alkynes oralkenes.

The process can also be utilized in the process of cracking of a liquidhydrocarbon composition by converting certain products of conventionaloil distillation; e.g., naphtha and others; into highly branchedalkanes. With respect to naphtha, naphtha is heated only to the point ofvaporization followed up by the electron beam process to realize theconversion of the obtained vapors mixed with natural gas and otherenhancing gaseous additives into highly branched liquid alkanes.

Lastly, the process can be utilized in cleaning up industrial fluegases.

FIG. 8 illustrates an example of a dual electron beam sustained plasmadischarge system which can be utilized to separate oil from water or totreat contaminated water.

As illustrated in FIG. 8, two electron beam generators 30 are positionopposite each other. Contaminated water (water/oil mixture) enters acavitation unit 10 where the contaminated water is cavitated with air tocreate an air-bubble filled mixture. The cavitation process breaks upthe bubbles down to small and smaller bubbles so that the effectivesurface area of the bubbles is increased.

In an oil recovery system, the oil will retain more of the bubbles thanthe water.

The cavitated mixture is ejected from the cavitation unit 10 through theutilization of jet nozzles (not shown) to further facilitate thecavitation of the mixture with more air and smaller bubbles.

As the mixture is ejected, the electron beam generators 30 irradiate theejected mixture wherein the electron beam interacts with the air bubblesto generate ozone within the liquid water/oil droplets. The ozone caneffectively breakdown the oil hydrocarbons within the water. In otherwords, the air bubbles act as internal ozone generation sites whenirradiated by the electron beam.

It is further noted that while breaking down lighter components of crudeoil electron beam irradiation of oil in water mixture also promoteseffective consolidation of the heaviest components of crude oil such asasphaltenes and others into solid particulates. Exposure of water/oilmixtures to the electron beam irradiation doses in excess of 30 kGy (1kGy=1 kJ/kg) results in the effective precipitation of the solidparticulates formed from said heaviest hydrocarbon fractions of crudeoil.

The irradiated oil in water mixture passes over a filter 75 where thesaid heavy oil particulates can be effectively separated from the water.

It is noted that although FIG. 8 shows a horizontal electron beam systemfor irradiating a vertical path of a water mixture, the process iseffective on a horizontal water path by merely rotating the electronbeam system to create a vertical electron beam system.

FIG. 9 illustrates the effective power of a dual electron beam systemwith respect to the irradiated water column. For example, as theelectron beam 45 traverses the water column 500, the effective powerdeposition of the electron beam 47 (dash/dot line) diminishes

Moreover, as the electron beam 35 traverses the water column 500, theeffective power deposition of the electron beam 37 (dash/dot line)diminishes. However, by utilizing a dual beam system, as illustrated inFIG. 8, the overall effective power deposition of the electron beams 600(dash/dot/dot/dash line), upon individual diminishing, remainsrelatively high. Essentially, the entire column of water may experienceelectron beam irradiation at close to 100% utilization efficiency whenutilizing a dual beam system. In one embodiment, the energy of theelectron beam is 1.0 MeV.

FIG. 16 illustrates a block diagram of an oil recovery system using anelectron beam sustained plasma discharge system.

As illustrated in FIG. 16, the oil/water mixture is cavitated with airby a cavitation unit 4000. The cavitated mixture is irradiated by anelectron beam generation unit 5000. Thereafter, the irradiated mixtureis filtered to remove the water, by filter 6000.

In one embodiment, the cavitation process can be realized in three zonesor stages. In the first stage, air is introduced into the oil/waremixture. The air may be explosively introduced to the mixture (hightemperature and pressure). The first stage may create bubbles within themixtures having a diameter from 500 to 1000 microns.

In the second stage, the mixture is agitated to split the bubbles tosmaller and smaller sizes such that the bubbles have a diameter of abouta few microns. Such small bubbles effectively increase the surface ofthe bubbles, thereby allowing a greater access of the ozone generated inthe irradiation process to the oil contaminants in water.

In the third stage, the cavitated mixture is ejected through nozzles toadd more air to the mixture and further split the bubbles. The jettedmixture provides greater air saturation, more effective penetration ofthe electron beam, and greater generation of ozone in atomized explosivebubbles.

The nozzles may be conventional expansion nozzles or air can be added inthe jetting process (generating a jet spray).

The cavitation of air in the mixture and subsequent generation of ozoneinside the microbubbles of cavitated air by high energy electronsenables to increase the throughput of decontamination of water mixturesby 2-fold and more compared to e-beam irradiation alone withoutcavitation of air at given power of the electron beam.

FIG. 10 illustrates a block diagram system using a cavitation/electronbeam process to treat solid waste (sludge). As illustrated, solid waste(wet sludge), which has been processed by a digester 1000, is fed to acavitation/electron beam sustained plasma discharge unit 2000, where thewet sludge is cavitated and irradiated with an electron beam to producedewatered sludge.

The electron beam and cavitation treatment of wet sludge (both municipaland industrial) results in significant dewatering of both inorganicsediment particulates and so called bio-solids from water bound to theouter surfaces and inner surfaces of the pores of such particles in wetsludge (2-3% of total solid content-TSC).

It is noted that the electron beam and cavitation treatment is alsoeffective in removing bound water from partially dewatered (20-30% TSC)sludge coming from sludge dewatering centrifuges or belt presses.

It is also noted that just electron beam treatment, without cavitation,can provide sludge dewatering to a lower extent.

By utilizing electron beam treatment, significant energy savings canalso be realized over conventional dewatering processes by centrifuges,as well as, shipping costs due to the significantly lower water contentin the sludge.

FIG. 11 illustrates another block diagram system using acavitation/electron beam process to treat solid waste (sludge). In thissystem, a cavitation/electron beam sustained plasma discharge unit 3000is introduced before the digester 1000.

The cavitation/electron beam sustained plasma discharge unit 3000 breaksup the sludge so that the sludge does not require the same amount oftime in the digester 1000, thereby enabling the processing of moresludge during a given period of time.

As in FIG. 10, FIG. 11 illustrates that solid waste (wet sludge), whichhas been processed by a digester 1000, is fed to a cavitation/electronbeam sustained plasma discharge unit 2000, where the wet sludge iscavitated and irradiated with an electron beam to produce dewateredsludge.

The electron beam and cavitation treatment of wet sludge (both municipaland industrial) results in significant dewatering of both inorganicsediment particulates and so called bio-solids from water bound to theouter surfaces and inner surfaces of the pores of such particles in wetsludge (2-3% of total solid content-TSC).

It is noted that the electron beam and cavitation treatment is alsoeffective in removing water from partially dewatered (20-30% TSC) sludgecoming from sludge dewatering centrifuges.

It is also noted that just electron beam treatment, without cavitation,can provide dewatering to a lower extent.

By utilizing electron beam treatment, significant energy savings canalso be realized over conventional dewatering processes by centrifuges,as well as, shipping costs due to the lower water content in the sludge.

FIG. 12 illustrates a multiple electron beam system. In this example,the mixture to be irradiated is introduced into an oval chamber 80. Thechamber 80 includes windows 90 to allow irradiation by the electron beamgeneration units 30. The chamber 80 may also include cavitators (notshown) that cavitate the mixture between windows 90.

FIG. 13 illustrates another multiple electron beam system. In thisexample, the mixture to be irradiated is introduced into a circularchamber 85, through openings (not shown). The chamber 85 includeswindows 90 to allow irradiation by the electron beam generation units30. The chamber 85 may also include cavitators (not shown) that cavitatethe mixture between windows 90.

FIG. 14 illustrates a portable water shielding housing 5000 having asteel door 6000 to allow an entry way for personnel. This portable watershielding housing 5000 can be constructed to surround an electron beamgeneration unit 4000 so as to shield the environment from strayradiation. The housing may be constructed of bladders or pillows thatcan be filled on site with water to provide the shielding. The bladdersand pillows are designed to interlock together so that when stack, thewater-filled bladders or pillows create a stable wall.

FIG. 15 illustrates a portable water shielding housing 5000, which canbe constructed to surround an electron beam generation unit 4000 so asto shield the environment from stray radiation. The housing may beconstructed of bladders or pillows that can be filled on site with waterto provide the shielding. The bladders and pillows are designed tointerlock together so that when stack, the water-filled bladders orpillows create a stable wall.

By utilizing bladders and/or pillows which can be filled with water, theempty bladders and/or pillows can be centrally stored and easilytransported to a contamination site for construction. Moreover, by beingwater filled, heavy construction equipment is not required inconstructing the shield because the empty bladders and/or pillows can beplaced into their positions before filling.

With respect to converting lower molecular weight gaseous hydrocarbonmixtures into higher molecular weight highly-branched hydrocarbons,conventionally, methane, the main component of dry natural gas, is firstconverted to syngas mixture of CO+H₂ via steam reforming endothermicreaction:

CH₄+H₂O→CO+3H₂; ΔH=+49.2 kcal/mol

Syngas is a feedstock for many chemical processes, including productionof methanol and Fischer Tropsch (FT) synthesis. For these two processes,the desired syngas ratio is H₂/CO=2, which is the stoichiometry of thedirect oxidation exothermic reaction:

CH₄+0.5O₂→CO+2H₂; ΔH=−8.5 kcal/mol

Besides the more desirable H₂/CO ratio, direct oxidation reaction ismuch faster than steam reforming reaction with superficial contact timesof about 10 ms and 1 sec, in the respective reactions.

Conventionally, the industry focused on oxygen-driven conversion ofmethane such as direct oxidation of methane or indirect oxidation ofmethane such as in FT synthesis, while non-oxidative methane conversionreceived less attention.

Direct oxidation conversion of methane typically involves partialoxidation to methanol or conversion to C₂+ hydrocarbons, primarilyethane C₂H₆ or ethylene C₂H₄ via oxidative coupling process. Theoperating parameters for these two conversions are different: oxidativecoupling (OC) is normally carried out at lower total pressure P=0.1 to0.5 MPa and elevated temperatures T>700° C., while direct partialoxidation (DPO) is typically performed at much higher pressure P=5 to 8MPa and lower temperatures T<475° C. At mixed conditions at totalpressure P=6.2 MPa and moderate temperature T=550-600° C., increasingoxygen partial pressure and temperature favors C₂+ pathway whilereducing both parameters favors methanol. The main drawback of directoxidation is its low selectivity towards C₂+ due to the competingreactions of carbon atoms with oxygen resulting in CO and CO₂.

Non-catalytic non-oxidative conversion of methane at high gastemperatures T>900° C. results in low selectivity towards C₂+ formationdue to extensive generation of solid black carbon and molecularhydrogen. One step catalytic conversion of methane to higher molecularweight hydrocarbons in non-oxidative H₂/He carrier gas has been achievedusing Pt—Co/NaY bimetallic catalyst at lower temperature T=250° C. This“one-step” process is primarily assigned to the metallic cobaltparticles whose reduction is facilitated by the presence of platinum.

A high selectivity one-step conversion of methane to C2+ hydrocarbons inoxygen-free environment and to methanol at oxidative conditions has beendemonstrated using partially-ionized non-equilibrium plasma atatmospheric pressure and ambient temperatures generated in methane usingnon-thermal plasma discharges such as dielectric barrier discharge (DBD)and pulsed corona discharge.

Furthermore, availability of high energy gamma, beta (electrons), oralpha particle radiation sources present another approach for conversionof low molecular weight hydrocarbons to higher molecular weighthydrocarbons. For example, methane radiolysis by alpha particlesemanated from radon gas results in reduced total gas pressure, formationof hydrogen, ethane, propane, butane, and pentane and a small amount ofhigher liquid hydrocarbons.

Methane irradiated by electrons shows qualitatively similar results toirradiation by the nuclear radiation with the formation of hydrogen,ethane, and higher molecular weight hydrocarbons, with a very slightchange in total gas pressure. The primary products (positive ions andfree radicals) resulting from reactions induced in methane by 100 eVelectrons are produced in nearly equal amounts, 45% and 55%,respectively.

A gas to liquid fuels conversion of hydrocarbon gas mixtures in oxygenfree environment is driven by free radicals and molecular ions generatedin the gas mixtures either by electron beam alone or by electron-beamcombined with non-thermal plasma discharge, such as pulsed dielectricbarrier discharges, corona discharges, glow discharges, gliding arcdischarges, etc.

Such electron beam or electron-beam combined with non-thermal plasmadischarge driven conversions of gaseous feedstock are further enhancedby hydrocarbon branching initiating substances; such as admixtures withlight alkynes such as acetylene (C₂H₂), methyl acetylene (C₃H₄),dimethyl acetylene (C₄H₆), propane, and light alkenes such as ethylene(C₂H₄), propene (C₃H₆), butane (C₄H₈), etc.

In another embodiment, the hydrocarbon gas is comprised of natural gasenriched with higher molecular weight hydrocarbons such as straight rungasoline, naphtha, bitumen, etc. derived from distillation of crude oil.

In a further embodiment, the gas to liquid fuels conversion feed stockmay contain hydrogen sulfide (H₂S).

In an electron beam conversion of gaseous feedstock driven or anelectron-beam combined with non-thermal plasma discharge drivenconversion of gaseous feedstock carried out at above atmosphericpressures and relatively low gas temperatures (T<300° C.), alkylation oflight olefin additives; such as addition of methyl and higher alkylradicals to ethylene, acetylene, or propene; takes place concurrentlywith dissociation and ionization of ethylene (C₂H₆) or acetylene (C₂H₄)with later leading to formation of the highly reactive acetylene ions(C₂H₄)⁺ and highly reactive methyl dyne (CH), as well as CH₂ and C₂Hradicals.

The CH radical readily reacts with other unsaturated hydrocarbons; suchas acetylene, ethylene (C₂H₄, alkene (C₃H₄, CH₂CCH₂), propane (C₃H₄,CH₃CCH), and propene (C₃H₆); resulting in active branching orisomerization

In all of these cases, the dominant product channels are characterizedby loss of an H-atom, following CH addition, forming a general patternfor the reaction of CH with small unsaturated hydrocarbons:

CH+C_(n)H_(m)→C_(n+1)H_(m)+H

In case of the CH+C₃H₆ reaction, 1,3-butadiene isomer of C4H6 is themajor product, and non-negligible quantities of 1,2-butadiene and1-butyne are also formed.

The presence of hydrogen sulfide (H₂S) in the feedstock gas may alsoaffect rates of electron beam conversion of gaseous feedstock driven orelectron-beam combined with non-thermal plasma discharge drivenconversion of gaseous feedstock and influence selectivity of thehydrocarbon conversion

More specifically, the presence of hydrogen sulfide (H₂S) in thefeedstock gas may change the rate and selectivity during the pyrolysisof ethane, propane, methyl propane, butane, dimethyl propane, decane,I-dodecane, butyl benzene, tetralin, hexadecane, with hydrogen sulfideacting as a catalyst, replacing the slow rate of hydrogen transfer bymore rapid reactions.

Other embodiments of an electron beam conversion of gaseous feedstockdriven or an electron-beam combined with non-thermal plasma dischargedriven conversion of gaseous feedstock may include natural gas blendedwith various pyrolysis gases obtained from pyrolysis of coal, biomass,municipal waste, etc.

The disclosed electron beam sustained non-thermal plasma dischargeallows for a steady sustainable non-thermal plasma environment atatmospheric and above atmospheric gas pressures, thereby enablingindustrial scale electron-beam driven gas to liquid fuel conversion.

Electron beam sustained non-thermal plasma discharges allow conversionof high-pressure gas mixtures without special additives with lowionization potential

In one embodiment, a high power e-beam is combined with a high voltagedielectric-barrier discharge. The dielectric-barrier discharges arecharacterized by the presence of insulating layers between metalelectrodes surrounding the discharge space, in addition to insulatingthe metal electrodes such that the dielectric barrier provides aninsulation of the manifold of gas to liquid fuel reactor from chemicallyactive gas under electron beam or electron-beam combined withnon-thermal plasma discharge radiolysis.

In a further embodiment, metal electrodes can be imbedded inside theinsulating dielectric layers. Moreover, different planar or cylindricalconfigurations may be deployed.

The presence of the dielectric(s) precludes dc operation, thus a typicaloperating range for dielectric-barrier discharge is 0.5 kHz to 500 kHz.

For self-sustained atmospheric pressure discharge and voltage at 10 kV,gap spacing is limited to less than 1 cm. However, when the highervoltage 10 kV to 100 kV discharge is initiated at and sustained byintense electron beam, the gap space may be increased significantly.

An e-beam-sustained non-thermal plasma discharge conversion processoptimizes the energy deposited into the gas by the non-thermal plasmadischarge system versus the energy deposited by the electron beam, ase-beam accelerators are generally more expensive per kW power thanplasma discharge generators. Such optimization also takes into accountvery high 90-95% wall plug efficiency of modern low-to-medium electronenergy 0.5 MeV to 2.5 MeV electron accelerators versus only 50-55% wallplug efficiency of some 10 kV to 100 kV non-thermal plasma dischargedevices.

Non-thermal plasma discharges driven by e-beam also maintains good spacelocalization and homogeneity of the ionized gas (plasma) that serves asan efficient catalyst to chemical reactions leading to polymerization oflower molecular weight C₂-C₄ gaseous alkanes of natural gas (methane,ethane, propane and butane) into highly branched higher molecular weightgasoline range alkanes (C₅-C₁₂) that are liquefiable at roomtemperatures (T<36° C.).

The e-beam/discharge processing of natural gas enriched with volatilehigher molecular weight components obtained from crude oil viae-beam/discharge induced cracking process may also be used to convertprimarily linear or slightly branched hydrocarbons into highly-branchedones with higher octane value.

It is noted that the e-beam-sustained non-thermal plasma dischargeconversion process may utilize multiple horizontal e-beams positioned onboth sides of a pressurized natural gas “pipeline.”

The e-beam-sustained non-thermal plasma discharge conversion process mayalso process feedstock gas under hydrogen depleted conditions achievedby prompt removal of hydrogen formed in the process of radiolysis of thefeedstock gas without replenishing feedstock gas pressure until thepoint of condensation of highly branched gasoline range fuel.

The e-beam-sustained non-thermal plasma discharge conversion process mayfurther feedstock gas under hydrogen depleted conditions achieved byprompt removal of hydrogen formed in the process of radiolysis of thefeedstock gas while replenishing feedstock gas pressure with highermolecular weight petroleum distillation product in products; such asstraight-run gasoline, naphtha, and bitumen heated above their boilingpoints.

As illustrated in FIG. 17, the above described processes and systems canbe implemented to convert biomass to liquid fuel.

In the illustrated example, E-beam-induced fast pyrolysis of abiomass/natural gas mixture takes place at moderate temperatures between400-450°.

The system of FIG. 17 includes a donut shaped biomass processing tank85. The biomass processing tank 85 includes windows to allow irradiationby the electron beam generation units 30. The chamber 85 may alsoinclude cavitators (not shown) that cavitate the mixture betweenwindows.

Dry small particulates of biomass are cyclone-whirled insidevaporization tanks 95 under a penetrating e-beam in the atmosphere ofnatural gas flowing through the biomass processing tank 85.

The use of natural gas as a carrier gas provides a stable anddiversified liquid fuel mixture by adding cross-linking and branching toboth straight chain and cyclic hydrocarbons

Biomass, such as algae or wood, should be dried and ground down to verysmall particulates to increase the overall surface area. This allows forfast vaporization and mixing with the carrier gas (natural gas) forbetter e-beam penetration of the mixture volume inside the biomassprocessing tank 85 at moderate electron energies of 1.5 MeV or less.

In the system of FIG. 17, the process involves a fast conversion ofbiomass into liquid bio-fuel in atmosphere of natural gas, absence ofoxygen. In addition to fast heating and vaporization of biomass, theprocess also involves generation of molecular ions and excited freeradicals and molecular polymerization taking place both in solid andvapor phases.

The vaporization tanks 95 are separated from the flow of the circulatingmixture of biomass vapors and carrier natural gas by membranes thatretain solid charred or charcoal particulates inside the biomassvaporization tanks 95. The mixture goes through a condenser (not shown)where the liquid fuel is collected while non-condensable gases such asH2 and CO2, etc. are separated from the natural gas/methane flow beforegoing through the next biomass vaporization tanks 95 on the oppositeside of the donut shaped biomass processing tank 85.

It is noted that the above described processes and systems can beimplemented to convert natural gas to a liquid fuel. In thisapplication, the electron beam non-thermal plasma conversion is used toconvert feed gas into highly branched liquid alkanes inside acirculation loop.

In this process, the feed gas may include dry Natural Gas, and wetNatural Gas or an associated petroleum gas. The feed gas may also bemixed with an energy transfer enhancing gaseous additive, such as argon,and/or a branching process enhancing gaseous additive, such as ethylene.

The feed gas is irradiated using the electron beam non-thermal plasmaconversion system/process to produce liquid products.

The process may include separation of the produced liquid product,comprising a mix of highly-branched alkanes, into individual componentsusing a distillation column followed by furtherpurification/condensation or condensation/purification depending on thesubstance and the methods of final purification.

It is further that the above described processes and systems can beimplemented to crack a liquid hydrocarbon composition resulting in theconversion of certain products of conventional oil distillation; e.g.,naphtha and others; into highly branched alkanes.

In this situation, naphtha is heated by electron beam irradiation to thepoint of vaporization followed up an electron beam non-thermal plasmaconversion of the obtained vapors, with natural gas and other enhancinggaseous additives, into highly branched liquid alkanes.

In addition, the above described processes and systems can beimplemented to clean-up of industrial flue gases. The industrial fluegases are irradiated using the electron beam non-thermal plasmaconversion system/process to produce liquid products. It is noted thatindustrial flue gases may be mixed with Natural Gas, wet Natural Gas oran associated petroleum gas, an energy transfer enhancing gaseousadditive, such as argon, and/or a branching process enhancing gaseousadditive, such as ethylene.

The process may include separation of the produced liquid product,comprising a mix of highly-branched alkanes, into individual componentsusing a distillation column followed by furtherpurification/condensation or condensation/purification depending on thesubstance and the methods of final purification.

The electron beam non-thermal plasma conversion system/process resultsin a mixture of high-octane (>100) highly-branched alkanes (saturatedhydrocarbons) with carbon chains C₆-C₁₂ that are liquid at roomtemperature and are highly valuable compared to straight-run gasolineobtained by the fractional distillation of petroleum that mostlyconsists of non-aromatic (aliphatic) linear hydrocarbons and commongasoline additives such as aliphatic highly-branched isooctane C₈H₁₈that is assigned an octane number of 100 and aromatics such as benzeneand methylbenzene (toluene) that have an octane number of 101 and103-106 respectively, while linear n-heptane is the zero point of theoctane rating scale.

In the refining process, the crude oil is converted into transportationfuels; such as gasoline, jet fuel, and diesel fuel; and other petroleumproducts, such as liquefied petroleum gas (LPG), heating fuel,lubricating oil, wax, and asphalt.

In the course of fractional distillation, crude oil is separated intofractions according to different boiling points of hydrocarbons ofvarying chain lengths. This fractional distillation process yieldsapproximately 25% of straight-run gasoline from each barrel of crudeoil.

Oil refinery products include jet fuel, diesel fuel and other petroleumproducts, such as liquefied petroleum gas (LPG), heating fuel,lubricating oil, wax, and asphalt.

Straight-run gasoline is a complex mixture of over 500 hydrocarbons thatmay have between 5 to 12 carbons. Smaller amounts of alkane cyclic andaromatic compounds are present. Virtually no alkenes or alkynes arepresent in gasoline.

Methylbenzene formed together with benzene and dimethyl benzenes(xylenes) during the catalytic reforming of C₆-C₉ naphthas accounts for90% of the methylbenzene (toluene) produced. Most of this methylbenzene(˜80%) is not separated, but is immediately mixed with petrol toincrease its octane number.

It is noted that xylenes present in the mixture have octane number of115-117.

As the consumption of lead-free gasoline increases, so does the demandfor the octane number upgrading additives.

It is noted that C₁-C₄ alkanes are in gaseous form; from C₅-C₁₇, thealkanes are liquids; and after C₁₈, the alkanes are solids understandard temperature and pressure conditions.

As the boiling point of alkanes is primarily determined by the length ofthe carbon chain, the boiling temperatures increase with increase of themolecular weight, rising about 20-30° C. for each extra carbon atomadded to the chain.

At a given amount of carbon atoms, a linear alkane will have a higherboiling point than its branched-chain isomers due to the greater contactsurface area, thus the greater van der Waals forces, between theadjacent molecules in the liquid phase.

For example, compare n-butane with isobutane (2-methylpropane) whichboil, respectively, at T=0° C. and T=−12° C. In case of two branchedhexane isomers 2,3-dimethylbutane ((C₆H₁₄) and 2,2-dimethylbutane(C₆H₁₄) that boil, respectively, at T=58° C. and T=50° C., two moleculesof 2,3-dimethylbutane have greater intermolecular van der Waals forcesdue to better ability to form an interlocking surface contact with eachother compared to the cross-shaped 2,2-dimethylbutane molecules.

In case of branched isomers of octanes, isooctane has the lowest boilingtemperature of T=99° C., while the most compact and most heavilybranched of 24 octane isomers tetramethyl butane has the boiling pointof T=106° C.

In contrast, the product of the electron beam non-thermal plasmaconversion system/process is predominantly saturated C₆-C₁₂hydrocarbons. The unsaturated hydrocarbons are formed only in thesecondary processes of decomposition of the saturated hydrocarbons inthe liquid droplets.

In one embodiment, the electron beam non-thermal plasma conversionprocess can be carried out under 1 MeV/50 mA electron beam at feed gaspressure P=1.5 atm, gas inlet T=30° C. The feedstock gas compositionsare shown in Table 1.

TABLE 1 GAS FEEDSTOCK COMPOSITION* Feedstock Mixture I Mixture IIComponents (NG) (HD5) Mixture III Methane (CH₄) 92.3 1.5 63.3 Ethane(C₂H₆) 3.6 2.0 8.4 Propane (C₃H₈) 0.8 91.0 9.2 Propene (C₃H₆) 0.0 3.0 0Butane (C₄H₁₀) 0.3 1.5 6.8 Isobutane (C₄H₁₀) 0.2 0.8 4.6 Pentane 0.0 0.02.8 Isopentane 0.0 0.0 2.6 Nitrogen 1.8 0.1 1.5 Carbon Dioxide 1.0 0.10.8 *Mixture I represents average natural gas composition in the US,mixture II represents composition of commercial propane gas (HD5) in theUS, mixture III represents flare gas or associated petroleum gas (APG)though APG composition particularly as it relates to methane/carbondioxide ratio may vary significantly from source to source.

The fractional composition of electron beam non-thermal plasmaconversion system/process liquid product is shown in Table 2.

TABLE 2 FRACTIONAL COMPOSITION OF AN ELECTRON BEAM NON- THERMAL PLASMACONVERSION PROCESS PRODUCT Fractionation Fractionation Distilled T [°C.] T [° C.] Fractions (Feed Gas Mixture I*) (Feed Gas Mixture II*)Initial boiling 36.1 36.1 point T [° C.] 10 wt % 65-69 66-71 20 wt %70-79 72-84 30 wt % 80-91 85-95 40 wt % 92-99  96-104 50 wt % 100-114105-116 60 wt % 115-127 117-134 70 wt % 128-140 135-149 80 wt % 141-169150-174 90 wt % 170   175-184 Terminal boiling 171-200 185-225 point T[°C.] Heavy Wax (wt %) <2   <3.0

The exposure of pressurized feed gas to intense electron beam alone orin combination with non-thermal plasma discharge results primarily inthe formation of the alkyl radicals with the unpaired electron localizedin the internal tertiary 3° C. or secondary 2° or C atoms as itslocalization on an external primary secondary 1° C. atom is much lesslikely.

In fact the 3°-H are inherently more reactive than 2°-H, and 2°-H areinherently more reactive compared to 1°-H by factors of 9:3:1respectively. This corresponds with alkyl radical stability: tertiaryradical species are more stable than secondary radical species, andsecondary radical species are more stable than primary radical species.

One of the leading reactions between two alkyl radicals isdisproportionation when instead of coupling they exchange a protonhaving one alkane and one alkene as the end products with the bond orderincrease by one over the reactants. The reaction is exothermic (ΔH=50-95kcal/mol=13-25 MJ/kg) and proceeds quite rapidly:

2CH₃—

H₂—₂C═CH₂+H₃C—CH₃

Alkene and Alkane Formation

When two different alkyl radicals disproportionate one acts as hydrogendonor while the other acts as hydrogen acceptor:

The efficient antiknock stability of the electron beam non-thermalplasma conversion system/process liquid product depends on the initialcomposition of feed gas. Lower octane values of final liquid product aretypical for the feed gas mixtures enriched in propane, n-butane, orn-pentane.

For example the prevalence of propane in the feed gas leads to increasedcontent of 2-methylpentane and 3-methylpentane that have relatively lowoctane values of 73 and 75 respectively. Recombination products ofn-butyl and n-amyl radicals also have low octane values3,4-dimethylhexane, 85; 3,4-diethylhexane, 62; 3-methyl-4-ethylhexane,68; 3,4-dimethylheptane, 56 and etc. The presence of such hydrocarbonslowers the efficient antiknock stability of synthesized liquids.

Some of some hydrocarbon components of the electron beam non-thermalplasma conversion system/process product mixture and its dependence onthe feed gas are shown in Table 3.

TABLE 3 ELECTRON BEAM NON-THERMAL PLASMA CONVERSION SYSTEM/PROCESSLIQUID PRODUCT AND SOME OF ITS INDIVIDUAL COMPONENTS LIQUID PRODUCTDensity MIXTURE Boiling Liquid Feed Gas Feed Gas [Condenser T_(B) [g/ml]at Mixture I Mixture II T = −42° C.] [° C.] 25° C. [wt %] [wt %]PENTANES (C₅H₁₂) 36.1 HEXANES (C₆H₁₄) 2,2-Dimethylbutane 50 0.649 0.050.14 2,3-Dimethylbutane 58 0.662 0.42 0.28 2-Methylpentane 62 0.660 0.380.28 3-Methypentane 64 0.660 0.13 0.28 n-Hexane 69 0.655 0.02 0.02 TotalHexanes: 1.0 1.0 HEPTANES (C₇H₁₆) 2,2-Dimethylpentane 78 0.674 0.05 0.112,4-Dimethylpentane 80 0.673 0.01 0.01 2,2,3-Trimethylbutane 80.9 0.6900.60 0.40 3,3-Dimethylpentane 86 0.693 0.11 0.04 2,3-Dimethylpentane 900.695 0.11 0.33 2-Methylhexane 91 0.679 0.02 0.02 3-Methylhexane 920.678 0.01 0.08 3-Ethylpentane 93.5 0.684 0.09 0.01 n-Heptane 98 0.0 0.0Total Heptanes: 1.0 1.0 OCTANES*(C₈H₁₈) 2,2,4-Trimethylpentane 992,2-Dimethylhexane 105.6 2,2,3,3- 106 Tetramethylbutane2,5-Dimethylhexane 108 2,2,3-Trimethylpentane 110 2,3,3-Trimethylpentane115 2,3-Dimethylhexane 116 2-Methylheptane 117 3-Methylheptane 120n-Octane 126 NONANES*(C₉H₂₀) 2,2,4-Trimethyhexane 125.52,2-Dimethylheptane 132 2,2,3-Trimethylhexane 133.72,3,3-Trimethylhexane 137.9 2,3-Dimethylheptane 140.8 3-Ethylheptane 143n-Nonane 151 DECANES*(C₁₀H₂₂) 2,2,3,3- 161.3 Tetramethylhexane2,3,4-Trimethylheptane 161.7 2-Methyl-3-Ethylheptane 161.9 2,2,3,4-162.2 Tetramethylhexane n-Decane* 174 UNDECANES*(C₁₁H₂₄)2,6-Dimethyloctane 159.7 3,5-Dimethyloctane 160 2,2-Dimethyloctane 1642,3-Dimethyloctane 164.5 n-Undecane 196 DODECANES* (C₁₂H₂₆)2,2-Dimethyldecane 201 2,2,3-Trimethylnonane 202 2,2,3- 212Pentamethylheptane n-Dodecane 216.2 *C₈, C₉, C₁₀ C₁₁ & C₁₂ alkanes have24, 35, 75, 159 & 355 isomers respectively.

The most volatile component of the electron beam non-thermal plasmaconversion system/process liquid product is n-pentane (C₅H₁₂) withhighest boiling point out of its three isomers T=36.1° C. thatcorresponds to initial boiling point of the electron beam non-thermalplasma conversion system/process mixture.

The product of electron beam non-thermal plasma conversionsystem/process, a liquid mixture of high-octane highly-branched alkaneswith octane numbers of individual components ranging from of 95-105 canbe immediately used as valuable octane number upgrading additive beforeits separation into individual components similar to toluene containingmixtures.

Alternatively, individual components in the electron beam non-thermalplasma conversion system/process product mixture can be separated,purified, and offered in the market for various industrial uses as wellas valuable research chemicals. The electron beam non-thermal plasmaconversion system/process produced liquid mixture primarily consists ofhighly-branched isomeric alkanes with very small amount of linearalkanes, not exceeding 3 wt %.

The efficient antiknock stability of the electron beam non-thermalplasma conversion system/process liquid product depends on the initialcomposition of the feed gas. Lower octane values of final liquid productare typical for the feed gas mixtures enriched in propane, n-butane, orn-pentane.

For example the prevalence of propane in the feed gas leads to increasedcontent of 2-methylpentane and 3-methylpentane that have relatively lowoctane values of 73 and 75 respectively. Recombination products ofn-butyl and n-amyl radicals also have low octane values3,4-dimethylhexane, 85; 3,4-diethylhexane, 62; 3-methyl-4-ethylhexane,68; 3,4-dimethylheptane, 56 and etc. The presence of such hydrocarbonslowers the efficient antiknock stability of synthesized liquids.

The feed gas mixtures with higher content of methane, ethane, isobutene,and neopentane lead to the high octane liquid product containing maincomponents such as 2,2,3,3-Tetramethylbutane, 2,2,3-Trimethylpentane,2,2,3-Trimethylbutane and 2,3,3-Trimethylpentane with octane values of103, 102, 101, and 100 respectively. The methyl and ethyl radicals,being the products of irradiation of methane and ethane, do not givebranched molecules by recombination with each other. However, thesesmall radicals are capable of generating strongly branched molecules dueto combinations with large alkyl radical, radical exchange or joining toalkenes.

The following fractions hexanes (C₆H₁₄), heptanes (C₇H₁₄), octanes(C₈H₁₈) and nonanes (C₉H₂₀) are distilled or boiled off at T=50-69° C.,T=78-94° C., T=99-126° C., and T=128-151° C. respectively. The terminalboiling point of decane isomers (C₁₀H₂₂) is T=174° C.

The distillation of undecanes (C₁₁H₂₄) is completed at T=196° C. that isthe terminal boiling point temperature indicating the presence ofundecanes in the liquid product. The terminal distillation point ofdodecanes is T=216° C. (see Table 4).

TABLE 4 MELTING & BOILING POINTS OF C₁-C₁₂ ALKANES Molecular MeltingPoint Boiling Point Name Formula (° C.) (° C.) methane CH₄ −183 −164ethane C₂H₆ −183 −89 propane C₃H₈ −190 −42 butane C₄H₁₀ −138 −0.5pentane C₅H₁₂ −130 36 hexane C₆H₁₄ −95 69 heptane C₇H₁₆ −91 98 octaneC₈H₁₈ −57 125 nonane C₉H₂₀ −51 151 decane C₁₀H₂₂ −30 174 undecane C₁₁H₂₄−25 196 dodecane C₁₂H₂₆ −10 216

The C₁₂H₂₆ and C₁₃H₂₂ fractions have higher boiling temperatures of 216°C. and 235° C. respectively. The total content of the heavy alkanes,so-called still bottoms, in the synthesized liquid mixture does notexceed 2-3 wt % (see Table 2 above).

The measured fractional composition of the synthesized liquid is fairlyclose to the typical compositions of commercial gasoline mixtures.

It is noted that natural gas consists of hydrocarbons that remain in thegaseous phase at temperature T=288.15 K (15.15° C., 59.27° F.;) andatmospheric pressure P=101.325 kPa (1 atm; 14.696 psi), considered to beinternational standard temperature and pressure (ISTP) conditions fornatural gas and similar fluids [Natural gas-Standard ReferenceConditions (ISO 13443): International Organization for Standardization.1996, Geneva, Switzerland.]

This effectively limits the definition of natural gas to fourhydrocarbon components: methane (C₁H₄), ethane (C₂H₆), propane (C₃H₈),and two butanes (C₄H₁₀): n-butane and iso-butane (2-methylpropane) aswell as small percentage of atmospheric gases such as nitrogen (N₂) andcarbon dioxide (CO₂)

Natural gas reservoirs may also contain heavier hydrocarbons oftenreferred as natural gas condensates beginning from pentane (C₅H₁₂) thatare liquid at standard temperature and pressure, but may exist ingaseous phase in the reservoir.

However, components heavier than hexadecane (C₁₆H₃₄) produced as liquidor solid waxy compounds are not considered as part of natural gascondensate.

Average natural gas composition in the US, according to Gas TechnologyInstitute 1989-1992 survey data containing 7000 natural gas samples, isas follows: 92.3% methane (CH₄), 3.6% ethane (C₂H₆), 0.8% propane(C₃H₈), 0.5% butane (C₄H₁₀), 1.8% nitrogen (N₂) and 1% carbon dioxide(CO₂).

Natural gas with the listed above average composition has mass densityd=0.74 kg/m3 (molar mass=17.48 kg/kmol) at STP conditions. Natural gascompressibility factor Z changes with pressure from Z=0.9978 at P=0.1MPa (1 atm) to 0.8916 at P=5 MPa (50 atm) at constant temperatureT=15.15° C. Natural gas mass density variation with increase of pressureis shown in Table 5 at two temperatures T=15.15° C. and T=75.75° C.

TABLE 5 NATURAL GAS DENSITY AT VARIOUS PRESSURES AND TEMPERATURESP[MPa]/T[° C.] 0.1/ 01/ 0.5/ 0.5/ 1.0/ 1.0/ 5.0/ 5.0/ 15 75 15 75 15 7515 75 d[kg/m³] 0.74 0.60 3.69 3.03 7.46 6.09 40.89 31.67

The electron beam non-thermal plasma conversion system/process providesfor an efficient process of converting natural gas to high octane (100+)gasoline-like fuel additive.

For example, the electron beam non-thermal plasma conversionsystem/process input is natural gas (NG) with a lower heating value(LHV) of 46 MJ/kg and energy expenditures per unit of liquid fuel (LF)product: electron beam energy of 15 MJ/kg

OUTPUT is 86 wt % Liquid Fuel (LF with LHV=46 MJ/kg) plus 11 wt %hydrogen gas (H2 with LHV=120 MJ/kg) and 3 wt % of heavy wax (HWX) withLHV=46 MJ/kg.

The mass balance is NG [1 MMcf=20 MT]

LF [17.2 MT=150 BBL]+H2 [2.2 MT]+HWX [0.6 MT].

The energy balance is NG [20 MT×46 GJ/MT=940 GJ]+EE [15 GJ/MT×17.2MT=258 GJ]

LF [45 GJ/MT×17.2 MT=774 GJ]+H2 [120 GJ/MT×2.2 MT=264 GJ]+HWX [0.6 MT×45GJ/MT=27 GJ]+Q [133 GJ heat losses].

The electron beam non-thermal plasma conversion system/process may alsogenerate hydrogen gas.

The electron beam non-thermal plasma conversion system/process is alsoapplicable to conversion of biomass to liquid. In the biomass to liquidprocess, bio-oils are generated by flash pyrolysis and hydrogenation andcracking of bio-oils occur simultaneously.

The electron beam non-thermal plasma conversion system/process can beutilized on site where the source of natural gas and/or biomass isavailable saving on transportation costs. Electricity can be generatedby turbine fueled by natural gas.

An integrated bio/fossil-fuel refinery & gas to liquid system driven byionization energy source utilizes powerful high-energy electron beamcombined with non-thermal plasma discharge to convert a large variety offeed stocks ranging from natural gas to lignocellulosic biomass to lowergrade oil refinery products to coal and shale particulates andcombination thereof to a range of output products such as liquid fuelsfrom gasoline to jet fuel to diesel range, hydrocarbon specialtychemicals, hydrogen gas and hydrogen enriched natural gas (HENG)

The entire system may be powered by electricity supplied by the grid orstand-alone generators including gas turbines powered by natural gas ortown gas or hydrogen-enriched natural gas produced on the site.

The main component of the disclosed liquid fuel producing system is highpower high wall-plug efficiency electron beam accelerator providingscanned over the e-beam at the electron energy range between E=0.5-5MeV, preferably between E=0.5-2.5 MeV and most preferably betweenE=0.5-2.5 MeV and electron current between 10 mA-1000 mA, preferablybetween 100 mA-1000 mA.

The e-beam output/input window of the accelerator is tightly integratedinto the walls of the conversion reactors, both solid to vapor andnatural gas/vapor to liquid fuel conversion reactors with the e-beamoutput/input windows positioned either along the flow of the medium oracross the flow of the medium that is irradiated by high energyelectrons inside the reactors.

The e-beam energy, the size of the e-beam output window, the workingvolume of the reactor(s) and the average specific gravity of the mediumintended for the conversion and exposed to e-beam are chosen to assurethe most effective deposition of the entire e-beam energy in suchmedium.

The accelerating tubes and insulation tanks of the electron acceleratorsmay be also positioned ether horizontally or vertically in regards tothe land notwithstanding the position of their respective e-beam outputwindows or the medium flow in the reactors.

The e-beam irradiated feedstock medium may comprise solid organicparticulates alone placed inside a fixed-bed reactor, a packed-bedreactor, or a cone reactor, or solid organic particulates entrained in acarrier gas flow where carrier gas may be comprised of natural gas,methane extracted from gas hydrates, hydrogen enriched natural gas ormethane or produced gas.

Alternatively, e-beam irradiated feedstock medium may be comprised ofany hydrogen-rich carrier gas alone comprising natural gas, methaneextracted from methane hydrates, hydrogen enriched natural gas orhydrogen enriched methane or produced gas.

The electron beam non-thermal plasma conversion system/process may berealized by a first module constituting two sub-modules: a “condensedmatter to vapor” conversion reactor and a “char, gas and vaporseparation” system.

The first sub-module, the “condensed matter to vapor” conversionreactor, may comprise a fixed-bed reactor, a fluidized bed reactor, apacked bed reactor, a cone reactor, or any other type of reactortypically used for fast pyrolysis of biomass modified to incorporate thee-beam output/input window(s).

The first sub-module may comprise a free fall/entrained flow reactorwhere solid particulates of dry biomass are entrained in the flow ofcarrier gas comprised of natural gas, associated petroleum gas, hydrogenenriched natural gas.

Optionally, feedstock of lignocellulosic biomass may be enriched withessentially sulfur-free bitumen or bitumen vapor bitumen and/or anyother hydrogen-rich low value crude oil derivatives in solid, liquid orvapor phase.

The process by which essentially sulfur-free bitumen can be obtainedfrom the bitumen naturally containing sulfur or even man-madesulfur-enriched bitumen can be described as follows: first the sulfurcontaining solid bitumen is melted by electron beam to form a mixture ofliquid bitumen and liquid sulfur-enriched fluid, wherein the liquidbitumen has a lower specific gravity compared to liquid sulfur-enrichedliquid, and therefore, the liquids can be easily separated one fromanother.

In the second sub-module, the “char, gas and vapor separation” system,high molecular weight organic vapors, generated from of the biomassfeedstock via e-beam driven flash pyrolysis, are separated from theregular by-products of the pyrolysis including solid char particulatesand the low molecular weight gases. The vapor separation system mayinclude a cooling system to quench the reaction and condense the highmolecular weight organic vapors, or it may also comprise a gasseparation system.

The electron beam non-thermal plasma conversion system/process mayinclude another module, constituting a “gaseous matter to liquid”conversion reactor, wherein gaseous matter, comprised of high molecularweight organic vapors such as biomass vapors, are mixed with hydrogenenriched natural gas or natural gas alone.

In summary, the electron beam non-thermal plasma conversionsystems/processes described above can operate a versatile bio-fuelrefinery system converting a broad range of feedstocks into drop-infuels consisting of highly branched hydrocarbons. These may include jetfuel and diesel as well as certain valuable specialty chemicals.

The electron beam non-thermal plasma conversion systems/processes aredriven entirely by electricity and can be characterized as a flashpyrolysis system with very low carbon footprint.

To achieve flash pyrolysis, an external volumetric heating source isused in the form of high power electron beam instead of a conventionalapproach that involves a contact surface heating in one form or another.

The electron beam non-thermal plasma accelerator provides a high power,self-scanning 1 MW/1.5 MEV electron beam.

The e-beam driven flash pyrolysis system may be modular and scalable,and easily tunable for efficient processing of a wide variety offeedstocks.

The electron beam non-thermal plasma approach provides a solution tobiomass pyrolysis due to its rapid volumetric heating capacity ofbiomass particulates, and the high concentration of short-lived butextremely chemically active transient intermediaries generated in bothsolid and gaseous medium by the ionizing energy of the electron beam.

In the e-beam driven flash pyrolysis, the hydrogenation, as well ashydrocracking, is initiated early in the bio-oil vapor phase by ionizinge-beam radiation. Hydrogen for the process may be supplied via e-beamradiolysis of natural gas and/or low value oil refinery products such asheavy residue of bitumen added in the mix.

The presence of bitumen serves not only as a source of hydrogen forstabilization of bio-oils but also enhances compounds resulting fromcross reactivity between transient intermediates of lignocellulosicfeedstock and bitumen origin.

The presence of natural gas increases the generation of highly branchedhydrocarbons of lower molecular weight closer to gasoline range,allowing additional output flexibility based on the input mix.

As noted above, the process begins with generation of bio-oil vapors viaflash pyrolysis, with partial stabilization of bio-oil vapors takingplace in the volume of the first reactor. This is followed by rapidquenching and separation of bio-oil products from lower molecular weightgaseous content and charred, further followed by continuedhydro-treatment and hydrocracking of the bio-oil vapors via e-beamradiolysis

Electron beam radiolysis of bio-oil vapors enriched with natural gasgenerates a massive amount of free radicals leading to the well-knownphenomena of scission of long carbon chains as well as inducingbranching of their shorter intermediates. The vapors are extricated togenerate fuel.

A method for converting a gaseous hydrocarbon mixture intohighly-branched liquefiable hydrocarbons may enrich natural gas withacetylene; irradiate acetylene enriched natural gas with an electronbeam sustained non-thermal plasma discharge; cool irradiated gasmixture; and remove liquefied highly-branched hydrocarbons.

A method for converting long carbon chain fractions of crude oil intohighly-branched liquefiable hydrocarbons may include cavitating longcarbon chain fractions of crude oil with natural gas; irradiatingcavitated long carbon chain fractions of crude oil with an electron beamsustained non-thermal plasma discharge to create short carbon chainfractions; enriching short carbon chain fractions with natural gas;irradiating natural gas enriched short carbon chain fractions with anelectron beam sustained non-thermal plasma discharge; cooling irradiatedgas mixture; and removing liquefied highly-branched hydrocarbons.

A method for converting long carbon chain fractions of crude oil intohighly-branched liquefiable hydrocarbons may include cavitating longcarbon chain fractions of crude oil with natural gas; irradiatingcavitated long carbon chain fractions of crude oil with an electron beamto create short carbon chain fractions; enriching short carbon chainfractions with natural gas; irradiating natural gas enriched shortcarbon chain fractions with an electron beam; cooling irradiated gasmixture; and removing liquefied highly-branched hydrocarbons.

A method for converting long carbon chain fractions of crude oil intohighly-branched liquefiable hydrocarbons may include cavitating longcarbon chain fractions of crude oil with natural gas; irradiatingcavitated long carbon chain fractions of crude oil with an electron beamto create short carbon chain fractions; enriching short carbon chainfractions with natural gas; irradiating natural gas enriched shortcarbon chain fractions with an electron beam sustained non-thermalplasma discharge; cooling irradiated gas mixture; and removing liquefiedhighly-branched hydrocarbons.

A method for converting long carbon chain fractions of crude oil intohighly-branched liquefiable hydrocarbons may include cavitating longcarbon chain fractions of crude oil with natural gas; irradiatingcavitated long carbon chain fractions of crude oil with an electron beamsustained non-thermal plasma discharge to create short carbon chainfractions; enriching short carbon chain fractions with natural gas;irradiating natural gas enriched short carbon chain fractions with anelectron beam; cooling irradiated gas mixture; and removing liquefiedhighly-branched hydrocarbons.

A method for converting long carbon chain fractions of crude oil intohighly-branched liquefiable hydrocarbons, comprising cavitating longcarbon chain fractions of crude oil with natural gas; irradiatingcavitated long carbon chain fractions of crude oil with an electron beamsustained non-thermal plasma discharge to create short carbon chainfractions; enriching short carbon chain fractions with acetylene;irradiating acetylene enriched short carbon chain fractions with anelectron beam sustained non-thermal plasma discharge; cooling irradiatedgas mixture; and removing liquefied highly-branched hydrocarbons.

A method for converting long carbon chain fractions of crude oil intohighly-branched liquefiable hydrocarbons may include cavitating longcarbon chain fractions of crude oil with natural gas; irradiatingcavitated long carbon chain fractions of crude oil with an electron beamto create short carbon chain fractions; enriching short carbon chainfractions with acetylene; irradiating acetylene enriched short carbonchain fractions with an electron beam; cooling irradiated gas mixture;and removing liquefied highly-branched hydrocarbons.

A method for converting long carbon chain fractions of crude oil intohighly-branched liquefiable hydrocarbons may include cavitating longcarbon chain fractions of crude oil with natural gas; irradiatingcavitated long carbon chain fractions of crude oil with an electron beamto create short carbon chain fractions; enriching short carbon chainfractions with acetylene; irradiating acetylene enriched short carbonchain fractions with an electron beam sustained non-thermal plasmadischarge; cooling irradiated gas mixture; and removing liquefiedhighly-branched hydrocarbons.

A method for converting long carbon chain fractions of crude oil intohighly-branched liquefiable hydrocarbons may include cavitating longcarbon chain fractions of crude oil with natural gas; irradiatingcavitated long carbon chain fractions of crude oil enriched natural gaswith an electron beam sustained non-thermal plasma discharge to createshort carbon chain fractions; enriching short carbon chain fractionswith acetylene; irradiating acetylene enriched short carbon chainfractions with an electron beam; cooling irradiated gas mixture; andremoving liquefied highly-branched hydrocarbons.

A method for removing petroleum from water may include cavitating thepetroleum/water mixture with air; irradiating the cavitatedpetroleum/water mixture with an electron beam sustained non-thermalplasma discharge to create ozone; and filtering the water from theirradiated mixture.

The petroleum/water mixture may be cavitated by introducing air into thepetroleum/water mixture to create air bubbles in the petroleum/watermixture; agitating the bubblified petroleum/water mixture to reducebubble size: and ejecting the bubblified petroleum/water mixture jetspray so that jet spray is irradiated with the electron beam sustainednon-thermal plasma discharge.

The jet spray may be generated by an expansion nozzle.

The jet spray may be generated by a nozzle and pressurized gas.

A method for treating solid waste may include processing the solidwaste, using a digester, to create wet sludge; and cavitating andirradiating the wet sludge with an electron beam sustained non-thermalplasma discharge to dewater the sludge.

A method for treating solid waste may include processing the solidwaste, using a digester, to create wet sludge; and irradiating the wetsludge with an electron beam sustained non-thermal plasma discharge todewater the sludge.

A method for treating solid waste may include cavitating and irradiatingthe solid waste with an electron beam sustained non-thermal plasmadischarge; processing the irradiated solid waste, using a digester, tocreate wet sludge; and cavitating and irradiating the wet sludge with anelectron beam sustained non-thermal plasma discharge to dewater thesludge.

A method for treating solid waste may include cavitating and irradiatingthe solid waste with an electron beam sustained non-thermal plasmadischarge; processing the irradiated solid waste, using a digester, tocreate wet sludge; and irradiating the wet sludge with an electron beamsustained non-thermal plasma discharge to dewater the sludge.

A method for converting first carbon chain condensable fractions of wetnatural gas, the first carbon chain fractions having first carbonchains, into liquefiable highly-branched hydrocarbons cavitates firstcarbon chain condensable fractions of wet natural gas with natural gasto create a natural gas cavitated condensable fractions of wet naturalgas; irradiates the natural gas cavitated condensable fractions of wetnatural gas with an electron beam to create second carbon chainfractions, the second carbon chain fractions including carbon chainsshorter than the first carbon chains of the first carbon chainfractions; mixes the second carbon chain fractions with natural gasenriched with alkynes and alkenes to a create enriched natural gas andsecond carbon chain fractions mixture irradiates the enriched naturalgas and second carbon chain fractions mixture with an electron beamcombined with electron beam sustained non-thermal plasma discharge tocreate an irradiated gas mixture; cools the irradiated gas mixture tocreate a cooled irradiated gas mixture; and removes liquefiedhighly-branched hydrocarbons from the cooled irradiated gas mixture.

The wet natural gas may be blended with crude oil. The wet natural gasmay be a natural gas condensate.

A method for converting first carbon chain condensable fractions of wetnatural gas, the first carbon chain fractions having first carbonchains, into liquefiable highly-branched hydrocarbons cavitates firstcarbon chain condensable fractions of wet natural gas with natural gasto create a natural gas cavitated condensable fractions of wet naturalgas; irradiates the natural gas cavitated condensable fractions of wetnatural gas with an electron beam to create second carbon chainfractions, the second carbon chain fractions including carbon chainsshorter than the first carbon chains of the first carbon chainfractions; mixes the second carbon chain fractions with natural gasenriched with alkynes and alkenes to a create enriched natural gas andsecond carbon chain fractions mixture; irradiates the enriched naturalgas and second carbon chain fractions mixture with an electron beamsustained non-thermal plasma discharge to create an irradiated gasmixture; cools the irradiated gas mixture to create a cooled irradiatedgas mixture; and removes liquefied highly-branched hydrocarbons from thecooled irradiated gas mixture.

The wet natural gas may be blended with crude oil. The wet natural gasmay be a natural gas condensate.

A method for converting first molecular weight fractions of naturalpolymers derived from ground dry biomass into a diversified mixture ofliquefied organic compounds with added branching to both linear andcyclic monomers, the first molecular weight fractions of naturalpolymers derived from ground dry biomass being a higher molecular weightthan the diversified mixture of liquefied organic compounds with addedbranching to both linear and cyclic monomers, mixes solid particulatesof ground dry biomass with natural gas enriched with alkynes and alkenesto create the particulates and enriched natural gas mixture; irradiatesthe particulates and enriched natural gas mixture with an electron beamto create irradiated natural gas and the first molecular weightfractions vapors mixture; mixes irradiated gas and the first molecularweight fractions vapors with natural gas enriched with alkynes andalkenes to create an enriched natural gas and second molecular weightfractions vapors mixture, the second molecular weight fractionsincluding fractions with molecular weight smaller than the molecularweight of the first molecular weight fractions; irradiates an enrichednatural gas and second molecular weight fractions vapors mixture with anelectron beam combined with electron beam sustained non-thermaldischarge to create irradiated natural gas and vapors mixture; cools theirradiated natural gas and vapors mixture, to create a cooled irradiatedgaseous and vapors mixture; and removes liquefied fractions from thecooled irradiated gas and vapors mixture.

A method for converting first molecular weight fractions of naturalpolymers derived from ground dry biomass into a diversified mixture ofliquefied organic compounds with added branching to both linear andcyclic monomers, the first molecular weight fractions of naturalpolymers derived from ground dry biomass being a higher molecular weightthan the diversified mixture of liquefied organic compounds with addedbranching to both linear and cyclic monomers, mixes solid particulatesof ground dry biomass with natural gas enriched with alkynes and alkenesto create the particulates and enriched natural gas mixture; irradiatesthe particulates and enriched natural gas mixture with an electron beamto create irradiated natural gas and the first molecular weightfractions vapors mixture; mixes irradiated gas and the first molecularweight fractions vapors with natural gas enriched with alkynes andalkenes to create an enriched natural gas and second molecular weightfractions vapors mixture, the second molecular weight fractionsincluding fractions with molecular weight smaller than the molecularweight of the first molecular weight fractions; irradiates an enrichednatural gas and second molecular weight fractions vapors mixture with anelectron beam sustained non-thermal discharge to create irradiatednatural gas and vapors mixture; cools the irradiated natural gas andvapors mixture, to create a cooled irradiated gaseous and vaporsmixture; and removes liquefied fractions from the cooled irradiated gasand vapors mixture.

A system for removing petroleum from water, comprising a cavitator tocavitate a petroleum/water mixture with air bubbles; an electron beamgenerator to irradiate the cavitated petroleum/water mixture with anelectron beam to create ozone within air bubbles; and a filter to filterthe water from the irradiated mixture.

The cavitator may cavitate the petroleum/water mixture by introducingair into the petroleum/water mixture to create air bubbles in thepetroleum/water mixture; agitating the bubblified petroleum/watermixture to reduce bubble size; and ejecting bubblified petroleum/watermixture as a jet spray so that jet spray is irradiated with the electronbeam.

The jet spray may be generated by an expansion nozzle. The jet spray maybe generated by a nozzle and pressurized gas.

A system for removing petroleum from water, comprising a cavitator tocavitate a petroleum/water mixture with air bubbles; an electron beamsustained non-thermal discharge generator to irradiate the cavitatedpetroleum/water mixture with an electron beam sustained non-thermaldischarge to create ozone within air bubbles; and a filter to filter thewater from the irradiated mixture.

The cavitator may cavitate the petroleum/water mixture by introducingair into the petroleum/water mixture to create air bubbles in thepetroleum/water mixture; agitating the bubblified petroleum/watermixture to reduce bubble size; and ejecting bubblified petroleum/watermixture as a jet spray so that jet spray is irradiated with the electronbeam.

The jet spray may be generated by an expansion nozzle. The jet spray maybe generated by a nozzle and pressurized gas.

It will be appreciated that variations of the above-disclosedembodiments and other features and functions, or alternatives thereof,may be desirably combined into many other different systems orapplications. Also, various presently unforeseen or unanticipatedalternatives, modifications, variations or improvements therein may besubsequently made by those skilled in the art which are also intended tobe encompassed by the description above.

What is claimed is:
 1. A method for removing petroleum from water,comprising: cavitating the petroleum/water mixture with air bubbles;irradiating the cavitated petroleum/water mixture with an electron beamto create ozone within air bubbles; and filtering the water from theirradiated mixture.
 2. The method as claimed in claim 1, wherein thepetroleum/water mixture is cavitated by: introducing air into thepetroleum/water mixture to create air bubbles in the petroleum/watermixture; agitating the bubblified petroleum/water mixture to reducebubble size; and ejecting bubblified petroleum/water mixture as a jetspray so that jet spray is irradiated with the electron beam.
 3. Themethod as claimed in claim 2, wherein the jet spray is generated by anexpansion nozzle.
 4. The method as claimed in claim 2, wherein the jetspray is generated by a nozzle and pressurized gas.
 5. A method forremoving petroleum from water, comprising: cavitating thepetroleum/water mixture with air bubbles; irradiating the cavitatedpetroleum/water mixture with an electron beam sustained non-thermaldischarge to create ozone within air bubbles; and filtering the waterfrom the irradiated mixture.
 6. The method as claimed in claim 5,wherein the petroleum/water mixture is cavitated by: introducing airinto the petroleum/water mixture to create air bubbles in thepetroleum/water mixture; agitating the bubblified petroleum/watermixture to reduce bubble size; and ejecting bubblified petroleum/watermixture as a jet spray so that jet spray is irradiated with the electronbeam.
 7. The method as claimed in claim 6, wherein the jet spray isgenerated by an expansion nozzle.
 8. The method as claimed in claim 6,wherein the jet spray is generated by a nozzle and pressurized gas.
 9. Asystem for removing petroleum from water, comprising: a cavitator tocavitate a petroleum/water mixture with air bubbles; an electron beamgenerator to irradiate the cavitated petroleum/water mixture with anelectron beam to create ozone within air bubbles; and a filter to filterthe water from the irradiated mixture.
 10. The system as claimed inclaim 9, wherein said cavitator cavitates the petroleum/water mixture byintroducing air into the petroleum/water mixture to create air bubblesin the petroleum/water mixture; agitating the bubblified petroleum/watermixture to reduce bubble size; and ejecting bubblified petroleum/watermixture as a jet spray so that jet spray is irradiated with the electronbeam.
 11. The system as claimed in claim 10, wherein said jet spray isgenerated by an expansion nozzle.
 12. The system as claimed in claim 10,wherein said jet spray is generated by a nozzle and pressurized gas. 13.A system for removing petroleum from water, comprising: a cavitator tocavitate a petroleum/water mixture with air bubbles; an electron beamsustained non-thermal discharge generator to irradiate the cavitatedpetroleum/water mixture with an electron beam sustained non-thermaldischarge to create ozone within air bubbles; and a filter to filter thewater from the irradiated mixture.
 14. The system as claimed in claim13, wherein said cavitator cavitates the petroleum/water mixture byintroducing air into the petroleum/water mixture to create air bubblesin the petroleum/water mixture; agitating the bubblified petroleum/watermixture to reduce bubble size; and ejecting bubblified petroleum/watermixture as a jet spray so that jet spray is irradiated with the electronbeam.
 15. The system as claimed in claim 14, wherein said jet spray isgenerated by an expansion nozzle.
 16. The system as claimed in claim 14,wherein said jet spray is generated by a nozzle and pressurized gas.